Method for selective receipt of dimethylnaphthalenes

 

(57) Abstract:

The invention relates to a method for selective receipt of dimethylnaphthalenes isomerization of the initial mixture in the presence of a catalyst containing either beta-zeolite or an acidic crystalline zeolite ultrastable (with respect the Y-type having a molar ratio of the oxides of silicon and aluminum from 4:1 to 10: 1 and having a pore size provided dvenadcatiletnie oxygen cycles, and the size of the unit cell from to 24,2 24,7 at elevated temperature and pressure sufficient to maintain the mixture to the isomerization in the liquid phase. This method can improve the selectivity of the isomerization of methylnaphthalenes. 10 C.p. f-crystals., 6 table.

The invention relates to a method of producing dimethylnaphthalene, and in particular, offers a way of obtaining an individual isomer of dimethylnaphthalene of a mixture of isomers dimethylnaphthalene obtained by dehydrogenation of a mixture of dimethylaniline.

Dimethylnaphthalene is a necessary starting compound to obtain the corresponding naphthaleneboronic acid by oxidation.

Naphthalenesulphonate acids are the monomers that are known to be suitable for palokangas has better thermal stability and mechanical properties, than polyethylene terephthalate and useful in the production of films and rubbers.

Usually dimethylnaphthalene get when cleaning gases from coal in the form of a mixture of all ten possible isomers. However, the separation of these isomers is very time consuming and expensive. Therefore a method of obtaining individual isomers dimethylnaphthalene or a mixture of two or three isomers dimethylnaphthalene high purity and quality is highly desirable. One such method is a multistage synthesis, which includes: /1/ education alkenylbenzene the reaction of o-, m - or p-xylene with butadiene, /2/ the cyclization of the obtained alkenylbenzene with the formation of one or more dimethylethylene related to one or two of the three groups of isomeric dimethylethylene, group (A) contains 1,5 - 1,6 - 2,5 - and 2,6 - dimethylaniline, group (B) contains 1,7 - 1,8 - 2,7 - and 2,8 - dimethylethylene and group (C) contains 1,3 - 1,4 - 2,3 - 5,7 - 5,8 - and 6,7 - dimethylethylene, /3/ dehydrogenation of dimethylmethylene with the formation of the corresponding dimethylnaphthalene and /4/ isomerization obtained dimethylnaphthalenes to the desired isomer dimethylnaphthalene.

For example, in U.S. patents 3,775, 496; 3,775, 497; 3,775, 498; 3,775, 500 describes how cyclization samaratunga acid cyclization catalyst, such as acidic crystalline zeolites, such as silicon, aluminum, silicon and magnesium, and silicon-aluminum - zirconium and phosphoric acid, followed by dehydration of the obtained dimethylethylene in the vapor phase to the corresponding dimethylnaphthalenes in an atmosphere of hydrogen at 300 to 500oC and in the presence of solid catalysts, dehydrogenation, as noble metals on carriers and oxides homalomena, and then isomerization of each of the above dimethylnaphthalene in the desired isomer in the triad of dimethylnaphthalenes to which this isomer belonged when 275-500oC in the presence of a solid acid isomerization catalyst of the same type as described for the cyclization. On the other hand, cyclization and isomerization can be carried out in the liquid phase, in this case, the cyclization is carried out at 200-275oC solid postinoculation catalyst, at 70-140oC with an acid ion exchange resin, acidic crystalline zeolite, hydrofluoric or sulfuric acid or silicon porous catalyst.

In particular, U.S. patent 3,775,496 [1] describes the cyclization of 5-m-tolyl/-pentene-2 to 1.6 - and 1.8 - dimethylethylene, which then digitalout to 1.6 - and 1.8 - dim the>U.S. patent KZT 3,775, 497 [2] describes the cyclization of 5-phenylhexane-2 to 1.4 - dimethylethylene that digitalout to 1,4 - dimethylnaphthalene, which in turn isomerized 2.3 - dimethylnaphthalene.

U.S. patent 3.775.498 [3] describes the cyclization of 5-/o-tolyl/-pentene-2 - 1.5 - dimethylethylene, which is then digitalout to 1.5 dimethylnaphthalene, which in turn isomerized 2.6 - dimethylnaphthalene.

U.S. patent 3.775.500 [4] describes the cyclization of 5-/p-tolyl/- pentene-2 to 1.7 - dimethylethylene that digitalout to 1.7 - dimethylnaphthalene, which in turn isomerized 2.7 - dimethylnaphthalene. Ways isomerization dimethylnaphthalene disclosed in the following references:

U.S. patent 3.780.119 [5] describes a method of isomerization of dimethylnaphthalenes by using at 260oC mordenite catalyst in which the metal form of mordenite is present in 20% excess by weight, and the metal is selected from the group consisting of lithium, sodium, potassium, magnesium, calcium, strontium, barium, zinc and aluminum.

U.S. patent 3.803.253 [6] describes a method of hydroisomerization of dimethylnaphthalene by using a combination of hydrogenation catalyst and calcium-containing zeolite catalyst, takoh which describes a method of isomerization of dimethylnaphthalenes in the gas phase using a mixed catalyst, containing: // 65-95% by weight of the hydrogen form of mordenite in which more than 80% of the metal cations replaced by hydrogen ions and /b/ 5-35% by weight of a catalyst selected from the group consisting of Benoit and infusino the earth.

U.S. patent 3.885.328 [8] describes a method of isomerization of dimethylnaphthalenes when using aluminosilicate zeolite Y-type in liquid phase at 120-300oC. the Catalyst has an atomic ratio of aluminum-silicon of 0.1-1.0.

U.S. patent 3.888.938 [9] describes a method of isomerization of dimethylnaphthalenes in the liquid phase using a mixed catalyst containing: // 70-95% by weight of the hydrogen form of mordenite in which more than 80% of the metal cations replaced by hydrogen ions and /b/ 5-30% by weight of a promoter selected from the group consisting of Benoit and infusino the earth.

U.S. patent 3.928.482 [10] describes the selective isomerization of dimethylcarbinol, dimethylmethylene and dimethylnaphthalenes in the presence of an aluminosilicate zeolite containing cations of polyvalent metal in the exchange position, such as rare earth exchange zeolite type Y.

U.S. patent 3.957.896 (11) describes the selective isomerization of dimethylnaphthalenes in the presence of any type of natural or synthetic chemicalname, kremniiorganicheskie, infusoria earth, natural or synthetic mordenite, zeolites, X-type zeolite of A-type and zeolites L-type. These catalysts can be substituted for all or part of the hydrogen or metal. Moreover, these catalysts can be supported on a carrier or applied without him.

U.S. patent 4.524.055 [12] describes a crystalline aluminosilicate zeolite, which is used for the isomerization of dimethylnaphthalenes and has a molar ratio of silicon:aluminium 10:100, specific x-ray distances in the crystal lattice and the specific ratio of the adsorption of cyclohexane-n-hexane of at least 0,7.

U.S. patent 4.556.751 [13] describes the isomerization of dimethylnaphthalenes in the presence of a crystalline aluminosilicate having pentelow structure and the molar ratio of silicon: aluminum 12 and above. Moreover, the aluminosilicate may contain some other metals in the form of neomeniam metals.

The problem in all of these ways of previous works is the presence of other isomers dimethylnaphthalene, unreacted dimethylethylene and alkenylbenzene as impurities and by-products in the final desired asnosti and commercial value of the required isomer dimethylnaphthalene, especially as a source for obtaining naphthaleneboronic acid for use as a monomer in the production of polymers. Moreover, at high temperatures, used in gas-phase processes, the catalysts have a tendency relatively quickly deactivated. Thus, it is highly desirable to use a liquid-phase processes at a relatively low temperature and to improve the completeness and selectivity stage isomerization of dimethylnaphthalenes in the target product.

It is known that in the presence of acidic catalysts isomers of dimethylnaphthalene capable of isomerized within each triad of isomers dimethylnaphthalene, i.e., within 1.5 - 1,6 - 2,6 - dimethylnaphthalenes in the triad (A) 1,7 - 1,8 - and 2,7 - dimethylnaphthalenes in the triad (B) and 1,3 - 1,4 - and 2,3 - dimethylnaphthalene in the triad (C) it is Also known that the rearrangement dimethylnaphthalene isomers one of these triads in the other isomers of the triad occurs in a relatively lesser extent.

Therefore, it is highly desirable to increase the selectivity and completeness stages isomerization in the above-mentioned multi-stage method of obtaining specific desired isomer dimethylnaphthalene.

The aim of the invention is the creation of unattain.

The starting compounds in the process of isomerization of 2,6 - dimethylnaphthalene are 1,5 - 1,6 and 2,6-dimethylnaphthalene.

When the source for the cyclization stage is a 5-m-tolyl/ pentane-1 or -2, it is obtained 1,5-, 1,6 - 1,7-, 1,8-, 2,5-, 2,6 - 2,7- or 2.8-dimethylethylene or a mixture containing at least 80%, preferably at least 85% by weight of dimethylaniline, which in turn are the source and undergo dehydrogenation to the corresponding 1,5-, 1,6-, 1,7-, 1,8-, 2,6- and 2.7-dimethylnaphthalene, which are the initial stage of isomerization to obtain 2,6 - and 2,7-dimethylnaphthalenes. The corresponding 1,7-, 1,8 - and 2,7-dimethylnaphthalene are original in the process of isomerization of 2,7-dimethylnaphthalene.

The corresponding 1,3 - 1,4 - and 2,3-dimethylnaphthalene are original in the isomerization of 2,3-dimethylnaphthalene.

All of these original mix dimethylnaphthalene can be obtained by dehydrogenation of a mixture of the corresponding above-mentioned dimethylethylene in the liquid phase in the presence of a catalyst.

In the method of this invention, the isomerization reaction is conducted in the liquid phase at elevated temperature and under high pressure to ensure podderjanieoC, preferably from 240oC to approximately 300oC, preferably 280oC and in the range of pressure from about 0.5, preferably 0.8 to about 5, preferably of 1.3 ATA.

The isomerization reaction of this invention may be performed periodically or continuously.

The reaction apparatus used in each of the above stages may be any of known types: fixed bed, moving, fluidized, with a layer of catalyst suspended in the liquid phase, or by mixing solid particles in the liquid in the vessel. In General, however, the use of devices with a porous layer preferably commercially for further operations.

The increase in the conversion source and the selectivity of the formation of the desired product or range of products by the method of this invention is the result of the selected conditions of temperature and pressure, as well as high activity and selectivity of the used catalyst, which in turn allows the use of less stringent conditions, i.e., lower temperature and pressure, and this can be achieved by increased selectivity and reduced deactivation of the catalyst.

The catalyst used in the JV is sereveny or dealuminated crystalline aluminosilicate zeolite Y-type, having a molar ratio of silicon-aluminum from about 4:1, preferably from 5:1 to about 10:1, preferably 6:1 and having a pore size corresponding to dvenadtsatikolonnom oxygen cycle, and the dimensions of the unit cell approximately 24,2, preferably about 24.3 to 24,7, preferably of 24.6 angstroms. Suitable zeolites are products of Union carbide under the ciphers LZ-Y72 and LZ-Y20.

The isomerization catalyst preferably contains betazole. Composition, structure and method for producing beta-zeolite is described in U.S. patent 3.308.069. The structure of beta zeolite is also described in J. Haggin "Structure of Zeolite Beta Determined, in Chemical & Engineering News, p.23 (June 20, 1988). Beta zeolite is also an industrial product of PQ Corporation.

The above ultrastable (with respect zeolite Y-type, which can be used as the isomerization catalyst of the method of this invention, is in the protonated form and contains about 0.01, preferably from 1 to about 5, preferably up to 3 weight % of sodium, considering the elemental sodium to the weight of the zeolite.

Preferably the isomerization catalyst contains a hydrogenation component comprising metals of group VIII, of which more preferred palladium, platinum or Nickel.

If the isomerization is carried out periodically, the catalyst is used in the range of from about 0.1, preferably 1.0 to about 5, preferably 3 weight % of the zeolite component of the catalyst relative to the weight of the original dimethylnaphthalene, and the reaction time is about 0.5, preferably 2 to about 10, preferably 6 hours. If the isomerization is carried out in the continuous version, the space velocity is from about 0.1, preferably 0.5 to about 10, preferably 5 parts source dimethylnaphthalene one weight part of the zeolite component of the catalyst by weight per hour.

Examples 1-18.

The catalyst used in example 6, is available industrial silicon oxide-aluminum containing 13 wt%. aluminum. The catalyst used in Pro available industrial Union Carbide's LZ-Y72 in the hydrogen form, such as received from the manufacturer. The catalyst used in example 10, is industrially available Grace USY sieve containing 2.6% of sodium with the chemical and physical properties very similar to the product of the Union Carbide's LZ-Y72, and also suitable for use as catalyst in the cyclization process of dimethylmethylene, and at the stage of isomerization of the present invention. The original examples 1-15 served 1,5-dimethylnaphthalene in example 16-1,7 - dimethylnaphthalene and in examples 17, 18 - 1,4-dimethylnaphthalene. Table 1 concentration of 2,7 - DMN in the product adopted approximately equal concentrations of 1.7 - DMN and deducted from the amount of 2,6 - and 2,7 - DMN, which are determined in conjunction with the /to determine the concentration of 2,6 - DMN separately/. Effective maximum specific isomer DMN in the triad is the equilibrium concentration in the triad, which is usually equal to 40-45%.

Given in tables pressures in pounds per 1 DM2correspond to the quantities (kg/cm2), are given in table.A.

In each of examples 1-18 specific isomer dimethylnaphthalene used as the source, is mixed in the liquid phase with a catalyst without media in the reaction vessel with stirring and constant transmission erature reaction, and through various time intervals after initiation of select and analyse samples. Conditions of the experiments, the composition of the source and destination of products containing up to 13 carbon atoms, % conversion source and % selectivity education target products in each of examples 1-18 are presented in table. 1.

The catalyst used in example 1 is crystalline borosilicate molecular sieve /HAMS - IB Amoco Chemical/. The catalyst used in example 2, this Union Caride's LZ-Y20, ultrastable (with respect the Y-sieve containing 2 wt%. copper, counting on elemental copper. The catalyst used in example 3 is the Union Caride's LZ-Y62, newstructure sieve-type amaniampong form having dimensions of the unit cell 24.73 Catalyst used in examples 4 and 5, is available industrial Union Caride's LZ-Y82, ultrastable (with respect molecular sieve having a size of elementary cell 24.56 and the sodium content is less than 0.2 wt%. In example 4, this bolt was in the ammonium form and was not calcined. In example 5, the sieve was calcined before the formation of N-forms.

Example 19.

7.5 kg of distilled water, 7.5 kg of an aqueous solution containing 40 weight. CH hydroxide tetraethylene, 50 g of sodium hydroxide and 300 g of sodium aluminate dissolved in lane is rasego 40% of silicon oxide, mix in 10-gallon autoclave at 150oC, 72 h the mixture was filtered and the separated solid product is washed three times with distilled water, dried at 120oC and calcined at 538oC 4 h

The obtained dry powder contains 0.37% of the weight. sodium, considering the elemental sodium, and x-ray analysis shows that it has the diraction pattern of the beta zeolite. The following powder diffraction pattern of the product shows only those lines that are shared with all 4 samples of beta zeolite in U.S. Patent 3.308.069 (see tab. B).

This powder was used as the catalyst without ion exchange. A quantity of powder was subjected to ion exchange by the method of example 21 to reduce sodium, and after ion exchange the content of aluminum oxide, the molar ratio of the oxides of silicon and aluminum and the atomic ratio of silicon:aluminum were measured as to 1.14%, 68:1 and 34.1, respectively.

Example 20.

8 kg of distilled water, 8 kg of an aqueous solution containing 40 parts by weight of the hydroxide of tetraethylammonium, 3,81 kg of an aqueous solution containing 20 wt%. hydroxide of tetraethylammonium, 0.6 kg of sodium aluminate and 12.2 kg Zola ACS is nnow the mixture is filtered, and the separated solid product is washed three times with distilled water, dried at 120oC 16 hours and calcined at 538oC 6 hours.

The obtained dry powder contains 0,17% weight. sodium, considering the elemental sodium. X-ray diffraction analysis shows that this powder has an x-ray diffraction picture of the beta zeolite. The following powder diffraction pattern of the product shows only those lines that are shared with all 4 samples of beta zeolite in U.S. Patent 3.308.069 (see tab. B).

This powder was used as the catalyst without ion exchange. After ion exchange according to the method of example 21 for lowering sodium molar ratio of the oxides of silicon and aluminum and the atomic ratio of silicon : aluminium was 30:1 14.8:1, respectively.

Example 21.

2.3 kg pionneering powdered catalyst obtained in example 20, 4 kg of distilled water and 12 kg of an aqueous solution containing 19% ammonium nitrate mixed in a 22-liter flask with 72oC 4 h Then the mixture is cooled, the liquid is removed by decantation, and the obtained ion-exchange catalyst is then washed with water. The catalyst was dried at 120oC and so the /considering the elemental aluminum/ and the molar ratio of the oxides of silicon and aluminum and the atomic ratio of silicon to aluminum is 30:1 14.8:1, respectively.

163 g of dry powder of beta-zeolite, 454 g Sol of aluminum oxide containing 8.8% of the weight. solids and 123 g of distilled water, mix until a homogeneous mixture. This mixture is then incubated at 23oC 5 h, letting the liquid evaporate. Then the mixture is dried at 120oC 16 h and calcined at 538oC for 2 hours, obtaining a product containing 80% beta zeolite and 20% of alumina, which is then crushed and sieved, receiving a particle size of 20-40 mesh.

Examples 22-40.

In each of examples 22-40 some used original mix in the liquid phase with a catalyst without media under stirring in a reaction vessel with continuous transmission of a current of nitrogen to prevent the ingress of oxygen into the system. The weight ratio of the source and the zeolite component of the catalyst is 49:1 in each case. The pressure of the contents of the reaction vessel support is about 1 pound 1 inch2. The temperature of the reaction vessel was raised to the reaction temperature, and over different periods of time to select and analyse samples. Conditions of the experiments, the composition of the initial and final products, % 1,5-, 1,6 - and 2,6 - DMN triads in each of them, % 2,6 - DMN in each of 1,5-, 1,6 - and 2,6 - DMN triad, % reduction naftalina and trimethylnaphthalene in each of the examples 22-40 presented in table. 2-6.

The catalyst used in examples 22-24, is industrially available LZ-Y72 without media, such as received from the manufacturer Union carbide. The catalyst used in examples 25-28, is a beta-zeolite without the media having a relatively high ratio of silicon:aluminum and prepared according to example 19. The catalyst used in examples 29-37, is a beta-zeolite without the media having a relatively low ratio of silicon: aluminum and prepared according to example 20. The only sample of this catalyst was used in the four cycles in examples 32-37.

The catalyst used in examples 38-40, beta-zeolite, having a relatively low ratio of silicon - aluminum and obtained according to example 20, but in this case, low sodium due to ion exchange and applied on the basis of aluminum oxide according to example 21.

Comparing the results of tables 2 to 6 clearly shows that the use of beta-zeolite catalyst reduces the loss of 1,5-, 1,6 - and 2,6-dimethylnaphthalene - triad, reduces the formation of methylnaphthalenes, trimethylnaphthalenes and triad 1,7-, 1,8 - and 2,7 - dimethylnaphthalene compared using LZ-Y72 zeolite catalinahome relatively low ratio of silicon-aluminum, leads to increased formation of 2,6-dimethylnaphthalene and reduce losses triad 1,5-, 1,6 - and 2,6-dimethylnaphthalene compared with the use of beta-zeolite catalyst having a relatively high ratio of silicon, aluminum, and allows the use of lower reaction temperature or a higher temperature even when partially deactivated catalyst, compared with the use of LZ-Y72 zeolite catalyst.

From the above it is clear that the purpose of the invention is achieved. While there are only some decisions, other decisions and various modifications should be clear from the above descriptions are equivalent and are included in the scope of this invention.

1. Method for selective receipt of dimethylnaphthalenes isomerization original mix dimethylnaphthalenes, including isomerization of at least 20% of the total number of 1,5 - and 1,6-dimethylnaphthalene contained in the initial mixture (a) along with 2,6-dimethylnaphthalene, target 2,6-dimethylnaphthalene, 1,5-, 1,6 - 1,7 - and 1,8-dimethylnaphthalenes contained in the initial mixture (b) along with the 2,6 - and 2,7-isomers, in the target 2,7 - and 2,6-dimethylnaphthalene, 1,7 - and 1,8-dimethylnaphthalenes contained in the initial mixture (c) the outfit is a mixture of (d) with 2,3-dimethylnaphthalene, in the target 2,3-dimethylnaphthalene, wherein the initial mixture selected from the above, is subjected to the interaction in the liquid phase with a solid isomerization catalyst containing either beta-zeolite or an acidic crystalline zeolite ultrastable (with respect the Y-type having a molar ratio of the oxides of silicon and aluminum from 4 : 1 to 10 : 1 and having a pore size provided dvenadcatiletnie oxygen cycles, and the size of the unit cell from 24,2 to 24.7 angstroms, at an elevated temperature and pressure sufficient to maintain the mixture to the isomerization in the liquid phase.

2. The method according to p. 1, characterized in that at least 25% of the total number of 1,5 - and 1,6-dimethylnaphthalenes in the above initial mixture (a) will isomerized to 2.6-dimethylnaphthalene.

3. The method according to p. 1, characterized in that at least 25% of the total number of 1,5-, 1,6-, 1,7 - and 1,8-dimethylnaphthalenes in the above initial mixture (b) isomerized to 2,6 - and 2,7-dimethylnaphthalenes.

4. The method according to p. 1, characterized in that at least 25% of the total number of 1,7 - and 1,8-dimethylnaphthalenes in the above initial mixture (c) isomerized to 2.7-dimethylnaphthalene.

5. The method according to p. 1, characterized in that according to the 2,3-dimethylnaphthalene.

6. The method according to p. 1, wherein the isomerization is carried out at a temperature of from about 200 to about 300oC.

7. The method according to p. 1, wherein the isomerization is carried out at a temperature of from about 240 to about 280oC.

8. The method according to p. 1, characterized in that the isomerization catalyst contains beta-zeolite.

9. The method according to p. 8, characterized in that the isomerization catalyst contains a hydrogenation component comprising a metal of group VIII.

10. The method according to p. 1, wherein the isomerization catalyst is used without media.

11. The method according to p. 1, wherein the isomerization catalyst is applied on the inorganic carrier.

Priority signs:

24.06.88 - all the features of the invention except for the use as a catalyst beta zeolite;

27.02.89 - use as a catalyst beta zeolite.

 

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EFFECT: method provides improved conversion of methane into aromatic hydrocarbons.

15 cl, 5 ex

FIELD: basic organic synthesis, chemical technology.

SUBSTANCE: invention relates to the improved method for isomerization reaction of pentane-hexane fraction with aim for preparing high-octane additive for gasoline. Pentane-hexane fraction is subjected for isomerization reaction in reaction-rectifying process using a low-temperature platinum-alumina catalyst. The parent raw is subjected for preliminary separation for pentane and hexane fractions. These fractions are subjected for separate isomerization that is carried out in vapor phase in reaction zone in bottom of reaction-rectifying column. Catalyst is placed under plates of zone and pressure in reaction zone in maintained in the range from 0.6 to 3.6 MPa, temperature - from 110.0oC to 200.0oC in the mole ratio hydrogen : hydrocarbons at inlet into column from 0.03:1 to 4:1. Method provides enhancing conversion of n-pentane, n-hexane and methylpentanes to high-octane isomers, elevating octane number of isomerizate and constructive simplifying the process.

EFFECT: improved preparing method.

1 dwg, 1 ex

FIELD: petrochemical processes catalysts.

SUBSTANCE: catalyst based on crystalline element-alumino-phosphates and having structure A1PO-31 (SATO) is prepared by providing first reaction mixture containing aluminum source, phosphoric acid, and one or more sources of substituting element as well as organic structure-forming compound followed by crystallization of above mixture under hydrothermal conditions required to form crystals with structure A1PO-31 and isolation of solid crystallization product, to which further modifying group VIII metal is added. Structure-forming compound mentioned above is selected from di-n-pentylamine and mixture thereof with other di-n-alkylamines and substituting element is selected from magnesium, zinc, silicon, cobalt, manganese, nickel, and cadmium. Method of isomerization of n-paraffins at elevated temperature and hydrogen pressure in presence of above-described catalyst is also disclosed.

EFFECT: increased activity and selectivity of catalyst.

4 cl, 1 dwg, 3 tbl, 17 ex

FIELD: petrochemical processes.

SUBSTANCE: feedstock is brought into contact with preliminarily activated zeolite-containing catalyst, namely mordenite-supported Pt, at 250-300°C, pressure 1.5-3.5 MPa, hydrogen-containing gas-to-feedstock ratio 300-1000 nm3/m3, and feed flow rate 1.0-4.0 h-1. Preliminary activation of zeolite-containing isomerization catalyst is conducted in two successive steps: drying catalyst in inert gas flow; reducing catalyst in hydrogen-containing gas flow; and supplying feedstock and setting steady-state isomerization process. Drying of zeolite-containing catalyst in inert gas flow is effected under conditions of gradually raised temperature from 120°C at temperature raise rate 10-15°C/h and ageing for 2-5 h at 120°C to 350°C followed by ageing at this temperature, whereupon temperature is lowered to 130°C. Reduction of zeolite-containing catalyst in hydrogen-containing gas flow is effected at gradually raised temperature to 220-350°C at temperature rise rate 15-25°C/h and ageing for 2-6 h at 220-350°C, whereupon temperature is lowered to 180°C. Initial feedstock is supplied at 180°C in circulating hydrogen-containing gas flow, aged for 4 h at 180°C and then gradually heated to 250°C at heating rate 5°C/h, after which further heated at heating rate 5°C a day to achieve process characteristics meeting product quality requirements.

EFFECT: increased catalyst activity, selectivity, and working stability.

2 cl, 2 tbl, 17 ex

FIELD: petrochemical process catalysts.

SUBSTANCE: group of inventions relates to conversion of hydrocarbons using micro-mesoporous-structure catalysts. A hydrocarbon conversion process is provided involving bringing hydrocarbon raw material, under hydrocarbon conversion conditions, into contact with micro-mesoporous-structure catalyst containing microporous crystalline zeolite-structure silicates composed of T2O3(10-1000)SiO2, wherein T represents elements selected from group III p-elements and group IV-VIII d-elements, and mixture thereof, micro-mesoporous structure being characterized by micropore fraction between 0.03 and 0.40 and mesopore fraction between 0.60 and 0.97. Catalyst is prepared by suspending microporous zeolite-structure crystalline silicates having above composition in alkali solution with hydroxide ion concentration 0.2-1.5 mole/L until residual content of zeolite phase in suspension 3 to 40% is achieved. Thereafter, cationic surfactant in the form of quaternary alkylammonium of general formula CnH2n+1(CH3)3NAn (where n=12-18, An is Cl, Br, HSO4-) is added to resulting silicate solution suspension and then acid is added formation of gel with pH 7.5-9.0. Gel is then subjected to hydrothermal treatment at 100-150°C at atmospheric pressure or in autoclave during 10 to 72 h to produce finished product.

EFFECT: enlarged assortment of hydrocarbons and increased selectivity of formation thereof.

16 cl, 2 dwg, 2 tbl

FIELD: organic synthesis.

SUBSTANCE: invention pertains to obtaining branched alkanes with general formula CnH2n+2, where n = 4-10. CCI4 is gradually added to a mixture of hexane, triethylaluminium - Et3Al and a catalyst - PdCl2, in an argon atmosphere at atmospheric pressure and temperature of 10-60°C for a period of 0.5-2 hours. The molar ratio of hexane: Et3Al : CCl4 : PdCl2 is 75:10:20:0.1.

EFFECT: obtaining of a mixture of branched alkanes with high output.

1 tbl, 1 ex

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